RU2704196C2 - Tubular reactor and multi-phase polymerisation method - Google Patents

Abstract

FIELD: chemistry.SUBSTANCE: invention relates to a tubular reactor and a multi-phase polymerisation method, particularly to production of butyl rubber by polymerisation of monomers using a catalyst in a liquid solvent. Tubular reactor includes pipe section for radial limitation of reactor volume between inlet and outlet, mixer to create flow in axial direction of pipe section, wherein the mixer has such dimensions and can be operated such that a flow can be imparted to a centrifugal force which creates distribution of concentration in the radial direction inside the pipe piece, and outlet line for discharge of radially internal part of flow, made with possibility of movement in axial direction relative to pipe section. Method comprises mixing a first starting product with a second starting product and/or a polymerisation catalyst to form a product in a solvent using a stirrer, imparting centrifugal force to product and solvent by means of agitator and extraction of concentrated radial inner part of flow, wherein product has lower density than solvent.EFFECT: invention provides prevention of polymer particles adhesion to pipe section and reduced risk of blockage.21 cl, 3 dwg

Description

This invention relates to a tubular reactor by which multiphase polymerization can be carried out, as well as to a multiphase polymerization process. In particular, this invention relates to a tubular reactor, as well as a method for the production of butyl rubber by polymerization of monomers using a catalyst in a liquid solvent.

From EP 1,591,459 A1, it is known, by means of a tubular loop reactor (“loop reactor”), to carry out the polymerization for the production of polyolefins. For this purpose, a suspension is continuously withdrawn from the circulation reactor, which contains solid polymer particles in the solvent. The diverted stream is fed to the hydrocyclone so that the polymer particles are concentrated and then separated and cleaned in a separation device. The solvent separated in the separation device, as well as the fraction saturated with the solvent from the hydrocyclone, which was not supplied to the separation device, is again fed to the circulation reactor.

The disadvantage of such a reactor and a similar method is that individual pipelines and, in particular, the reactor can be easily clogged (clogged). In particular, in the production of butyl rubber, as a rule, it is necessary to carry out the polymerization at temperatures from -70 to -100 ° C. This temperature is close enough to the glass transition temperature of butyl rubber, which is approximately in the range from -75 to -67 ° C. Therefore, in particular, in the production of butyl rubber, there is the danger that due to the reaction heat generated during polymerization, the butyl rubber particles are no longer glassy and adhere very easily to surfaces in this state. This leads to clogging of the pipelines and in particular the tubular reactor, so it is often necessary to stop the production of butyl rubber and to make laborious cleaning of pipelines, as well as the tubular reactor.

The objective of the invention is to provide a tubular reactor, as well as a method for multiphase polymerization, in particular the production of butyl rubber, in which the risk of clogging is reduced.

According to the invention, the problem is solved by means of a tubular reactor, including at least a length of pipe for radially limiting the volume of the reactor between the inlet and outlet, an agitator for creating a flow in the axial direction of the length of the tube, and the agitator preferably has such dimensions and can be operated in this way that a centrifugal force can be imparted to the flow, which creates a concentration distribution in the radial direction inside the pipe section, and an outlet line for diverting the radially inner part n current.

In addition, the invention encompasses a method of multiphase polymerization, in particular the production of butyl rubber, comprising at least the following steps:

mixing the first starting product with the second starting product and / or the catalyst for polymerization to form the product in a solvent using a mixer, imparting centrifugal force to at least the product and solvent using the same mixer, and selecting a concentrated radially inner part of the stream.

The tubular multiphase polymerization reactor according to the invention, which can be used, in particular, for the production of butyl rubber, has a pipe section for radially limiting the volume of the reactor between the inlet and the outlet. The tubular reactor has an agitator to create a flow in the axial direction of the pipe section, the agitator according to the invention being so dimensioned that it can be operated in such a way that a centrifugal force can be imparted to the flow, which creates a radial concentration distribution inside the pipe section. In addition, an outlet line is provided for diverting the concentrated radially inner part of the stream.

Thus, by means of a tube reactor, not only axial flow and mixing of the first starting product with the second starting product and / or further starting products and / or catalyst is achieved, but also an additional centrifugal force is provided. In particular, the fraction of centrifugal forces exceeds the fraction of inertial and gravity forces in the axial direction, as well as the fraction of friction forces. Due to the imparted centrifugal force, a concentration distribution occurs inside the tubular reactor, so that already at least a partial separation of the product from the unreacted starting products and / or catalyst takes place inside the tubular reactor. In addition, the product can be concentrated, so that the product content in relation to the product / solvent mixture increases. Most preferably, the product has a lower density than the solvent, so that the product is concentrated in the interior of the tubular reactor. As a result, it is prevented that a product, for example, butyl rubber, comes into contact with a pipe section of a tubular reactor, so that particles of the product cannot adhere to the inside of the tubular reactor.

The risk of clogging the tubular reactor is therefore reduced. In addition, it is not necessary to supply the contents of the tubular reactor in addition to the hydrocyclone, since the action of the hydrocyclone can be achieved already inside the tubular reactor. This can be achieved using the same agitator that is already provided for achieving axial feed and mixing. It uses the knowledge that, also at the speed of the mixer, which are necessary in order to achieve a sufficiently large concentration of the product, a sufficiently turbulent flow is formed in the immediate vicinity of the mixer, which leads to good mixing of the used starting products / catalyst. In particular, in the production of butyl rubber, the reaction rate is so high that the residence time in the turbulent and mixed regions is sufficient in order to achieve a high degree of conversion and a good space / time yield. Peeling and concentration of the product occurs, in particular, in the production of butyl rubber only if the mixture is already close to chemical equilibrium. The geometry of the pipe section as well as the mixer can be selected in such a way that at least 60 percent by weight, in particular at least 80 percent by weight of the theoretically possible weight fraction of the product, which was calculated on the basis of chemical equilibrium, can be achieved.

Preferably, a biphasic layered rotating stream with at least two layers of different concentration can be generated in the area of separation agreed upon with the outlet within the pipe section. The mixer can be so dimensioned and operated in such a way that a layered rotating flow can occur inside the pipe section. For example, a Rankin vortex may occur inside a pipe segment. The layers of the rotating flow are separated from each other, in particular, by the phase boundary and can in each case have different angular velocities. As a result of this, partial volumes of various concentrations visually separated from each other arise. The geometry of the outlet line is adapted, in particular, to the expected geometry of the inner layer of the rotating stream. The outlet line may have, for example, an inner diameter that corresponds to the outer diameter of the inner layer, or a smaller diameter. As a result, it is ensured that a mass stream with the highest concentration of product can be diverted through the outlet line.

Preferably, the mixer is located near the entrance. In addition, a first supply line for introducing the first starting product and a second supply line for introducing the second starting product and / or catalyst may be provided, the first feeding line and the second feeding line entering the pipe section, in particular, next to the mixer. Further feed lines for the same source product and / or further feed lines for additional source products may also be provided. As a result of this, at the inlet of the pipe segment, a mixer can mix the starting products / catalyst with each other, so that the entire length of the tubular reactor can be effectively used. Premature polymerization in the feed lines is prevented so that too large particle sizes of the product can be prevented. Instead, by selecting the sizes of the pipe and mixer sections, the residence time of the mixed starting products / catalyst can be set so that the narrowest molecular weight distribution can be achieved. This facilitates in particular subsequent separation operations.

Most preferably, the outlet line is immersed within a pipe section in a concentrated radially inner part of the flow. The outlet line is made, for example, in the form of an immersion pipe, the inlet of which is located within the concentrated radially inner part of the stream. As a result of this, it can be prevented that behind the inlet of the pipe section of the tubular reactor, for example, due to a change in the cross section, cross-mixing of the concentrated product with the remaining components of the flow takes place.

The agitator is preferably an axial feed agitator that can impart centrifugal force to the flow. For this, the mixer is made, for example, in such a way that it can drive the feed stream into rotation. The mixer has, for example, a propeller, in particular, exactly one propeller, which, by analogy with the propeller of a ship, can create an axial flow and simultaneously a rotating flow. Through the rotating component of the flow, the mixer imposes a sufficiently large tangential force on the flow, so that the centrifugal force is imposed on the flow, which in the subsequent region of the tubular reactor can lead to delamination of the flow components.

In particular, the mixer is connected to the shaft, in particular to a perforated hollow shaft, preferably the shaft can be introduced into the tubular reactor through the shaft inlet, and the shaft inlet can be washed, in particular, with a solvent. Through the hollow shaft, the feedstock and / or catalyst may be fed into the tubular reactor. In addition, a return portion of the flow, for example, a concentrated solvent, can be conducted through the hollow shaft. Due to the perforation in the hollow shaft, the flow fed through the hollow shaft can interact and mix with the flow outside the hollow shaft before reaching the mixer. As a result, the feedstock and / or catalyst and / or solvent can be supplied to the tubular reactor both radially from the inside and radially from the outside. Due to the fact that preferably the solvent is fed through the shaft inlet, deposits are prevented and / or washed out.

Most preferably, the inner diameter D of the pipe section is adapted to the outer diameter d of the agitator. As a result, the gap between the pipe section and the mixer can be kept as small as possible without the risk of jamming the mixer in the pipe section. For this, for the ratio of the inner diameter D of the pipe segment to the outer diameter d of the mixer, the following 1.0001≤D / d≤1,300, in particular 1,0005≤D / d≤1,100 and preferably 1,001≤D / d≤1,010. For example, the D / d ratio is 1.005 ± 0.001.

Most preferably, the outlet line can move axially with respect to the length of the pipe. As a result of this, the outlet line can be adapted to different flow characteristics inside the pipe section, for example, if the mixer is to be operated with different speeds and / or different power consumption, and the product concentration is shifted in the axial direction of the pipe section. At the same time, the installation of a tubular reactor is simplified, as well as the installation of a tubular reactor in another apparatus, since the outlet line cannot collide with a pipe segment during installation. In addition, as a result, various types of product can be supplied.

The invention further relates to a heat exchanger, which has a tubular reactor, which can be designed and improved as described above. The tubular reactor is arranged essentially concentrically inside the heat exchanger, the heat exchanger radially outside the tubular reactor having at least one heat exchange element for heat removal. A tubular reactor stirrer can create a loop-like flow inside the heat exchanger. As a result, with just one mixer, it is possible to mix the starting products / catalyst, concentrate the product and provide a loop-like flow inside the heat exchanger. Due to the loop-shaped flow, for example, a solvent not removed through the outlet line can be supplied to the heat exchange elements in order to cool the solvent. Since most of the concentrated product has already been removed through the outlet line, the stream supplied to the heat exchange elements practically does not contain polymer particles that could adhere to the heat exchange elements. As a result, deterioration in heat transfer on the heat exchange elements is prevented. Replacement of the heat exchange elements and / or cleaning of the heat exchange elements can therefore be eliminated or, at least, carried out at significantly longer intervals. As a result, productivity is further improved. In addition, clogging of the transitions between the various heat exchange elements is prevented. Due to the preferred separation of the larger particles, clogging of the heat exchange elements themselves is prevented.

In a preferred embodiment, the outlet line has a cooling device for cooling the outlet line.

In particular, the cooling device preferably has a double-walled shell pipe for conducting a cooling medium. For example, the cooling medium may flow countercurrently along the exhaust line, rotate outwardly at the inlet of the intake line, and flow backward in the forward flow. Thanks to the cooled outlet line, the product can be prevented from heating up. In particular, in the production of butyl rubber, it is therefore prevented that concentrated butyl rubber does not remain glassy anymore due to the outlet line and adheres to the outlet line. As a result, clogging of the exhaust line is prevented.

The invention further relates to an apparatus for multiphase polymerization, which can be used, in particular, for the production of butyl rubber. The unit has a heat exchanger for cooling the fluid. In addition, the installation has a separation device for separating the product. A recycling line is connected to the output of the separation device and to the heat exchanger. The heat exchanger and / or recycling line has a tubular reactor, which can be designed and improved as described above. The outlet line of the tubular reactor is connected to the input of the separation device. The heat exchanger can be made and improved, in particular, as described above. Thanks to the tubular reactor, the polymer particles are prevented from sticking to the recycle line and / or to the heat exchanger elements and plugging them. The risk of clogging is therefore reduced, so that the installation can be operated more productively. In particular, it is possible to continuously operate the installation for a longer period of time, without the need for cleaning work. It is further possible to provide more than one heat exchanger, the heat exchangers being connected in series and / or in parallel, in order, for example, to separate the cooled mass flow into several smaller heat exchangers and / or to perform multi-stage cooling in order to achieve the largest temperature difference during cooling . In addition, it is possible to provide several connected in series and / or parallel separation devices in order to separate the mass flow of the product into several smaller separation devices and / or to perform multi-stage separation with the highest degree of purification. The separation device may have, in particular, an ultrafast evaporation unit, a light distillation column and / or a distillation column. Further, a purge line may be provided, which is connected in particular with a heat exchanger in order to prevent the concentration of harmful impurities in the solvent.

The invention further relates to a multiphase polymerization process, in particular for the production of butyl rubber, comprising the steps of: mixing a first starting product with a second starting product and / or a catalyst for polymerizing to form a product in a solvent using a stirrer, imparting a centrifugal force of at least at least the product and the solvent using the same mixer and the selection of concentrated radially inner part of the stream. Due to the fact that the mixer is used not only for mixing, but also for imparting centrifugal force, a radially concentrated inner part of the flow is formed, from which the concentrated product can be extracted. Since the product has in particular a lower density than the solvent, polymer particles that occur during polymerization can concentrate in the inner part of the stream, so that they cannot adhere to structural elements that limit the flow in the radial direction. As a result, the risk of clogging, in particular of tube-shaped structural elements, is reduced. Thus, the method can be continuously performed for a longer period of time without the need for cleaning and maintenance work. This leads to higher productivity of the method.

Preferably, when a centrifugal force is applied, a rotating stream is generated, the rotating stream being, in particular, a two-phase layered rotating stream with at least two layers of different concentration. Due to the rotating flow, the concentration of the product can be facilitated, due to which, in particular, it is possible to create two layers separated from each other by a phase boundary within the flow. This facilitates the selection of a concentrated product.

In particular, at least the solvent is cooled. The solvent is cooled, preferably after application of centrifugal force, and most preferably after selection of the concentrated radially inner part of the stream. As a result, it is possible to cool as little as possible of the polymer particles formed during the polymerization. Since heat transfer to the solvent is better than heat transfer to the polymer particles, more efficient cooling can be achieved as a result. In addition, the recovered chilled solvent can completely wash the polymer particles resulting from the polymerization, so that the removal of the reaction heat resulting from the polymerization from the formed polymer particles is the simplest and most effective. Most preferably, the solvent is supplied in a loop-like flow to at least one heat exchange element for heat removal, the loop-shaped stream being created preferably using the same mixer. As a consequence, only one mixer is required in order to provide the loop-like flow necessary for cooling the solvent. No additional feeder required.

Most preferably, the mixer is operated in such a way that for the ratio c = w _tan ² / ((d / 2) ⋅g), where w _tan is the tangential velocity at the outer edge of the mixer, d is the outer diameter of the mixer, and g is the acceleration free fall, the following is c≥10, in particular c≥100 and preferably c≥1000. Preferably c≤10000. With this operating mode of the mixer, it can be ensured that by means of the mixer not only mixing is achieved, but also concentration in the radially internal part of the flow created by the mixer.

Most preferably, the method uses a tubular reactor, which can be designed and improved as described above. Alternatively or additionally, a heat exchanger may be used in the method, which may be implemented and improved as described above. Alternatively or additionally, a method that can be implemented and improved as described above can be used in the method. By means of the tubular reactor used in this case, which is located, in particular, inside the heat exchanger, a suitable flow inside the pipe section of the tubular reactor can be forced to be forced by means of an appropriately actuated mixer, which after polymerization automatically leads to the concentration of the resulting product.

The invention will now be explained, by way of example, with reference to the attached drawing using preferred embodiments.

The drawings show:

figure 1 is a schematic side view of a heat exchanger with the corresponding invention, a tubular reactor;

2 is a schematic side view of a tubular reactor according to the invention in a further embodiment; and

figure 3 is a schematic side view of the installation for multiphase polymerization with a heat exchanger according to figure 1.

The heat exchanger 10 shown in FIG. 1 has a tubular reactor located concentrically with the middle axis 12. The tubular reactor 14 has a pipe section 16 that extends from the inlet 18 to the outlet 20. The tubular reactor 14 has a stirrer 22, referred to in the illustrated example implementation about the propeller. The mixer 22 is driven by a shaft 24, which protrudes from the bottom 26 of the heat exchanger 10. The shaft 24 is introduced into the heat exchanger 10 through the input 25 of the shaft, and through the input 25 of the shaft is supplied in particular a solvent in order to prevent and leach deposits. Using the shaft 24, the mixer 22 is loaded with a speed that is sufficient to create not only the axial flow 27, but also the rotating flow 28. Using the rotating flow 28, the centrifugal force is imparted to the axial flow 27, due to which a concentration distribution in the radial direction occurs inside the pipe section 16. This concentration distribution leads in the upper region of the tubular reactor 14, that is, near the outlet 20, to a layered rotating stream 28, which has an inner part 30 in which the product, in particular butyl rubber, is concentrated. Through the exhaust line 32, which is immersed in the inner part 30, the concentrated product can be recovered.

Part of the axial stream 27, which is not removed through the exhaust line 32, flows past the exhaust line 32 and deviates along the loop-shaped stream 34. The deflected loop-shaped stream 34, which is saturated in particular with solvent and catalyst, flows past the heat exchange elements 36, which cool the loop-shaped stream 34.

Next, at the bottom 26, through the first feed line 38, a first starting product, for example, a monomer, is supplied. A second feed and / or catalyst is supplied through a second feed line 40. The starting materials and / or the catalyst are dissolved, in particular, in a liquid solvent. By means of a mixer 22, the feeds / catalyst fed through the first feed line 38 and the second feed line 40 are mixed in the mixing zone 42 so that they can react with each other in the mixing zone 42. After this, the mixture from the product (reaction), initial products and / or catalyst enters the intermediate zone 44, in which the mixture can additionally react, but here delamination begins with a concentration distribution in the radial direction. In the swirl zone 46, a rotating flow is established, which has, in particular, an inner layer with an inner concentrated portion 30 and a solvent-saturated portion 48.

A recirculation stream can be supplied to stream 27 through a further supply line not shown, which was separated during cleaning of the concentrated product recovered through outlet line 32. In addition, the recycle stream can be supplied through the first supply line 38 and / or the second supply line 40. It is further possible to make the shaft 24 in the form of a hollow shaft and to supply the recirculation stream and / or the original product and / or the catalyst through the shaft 24 made in the form of a hollow shaft Preferably, the solvent is introduced through the inlet 25 of the shaft 24 in order to prevent and / or leach deposits.

Further, the heat exchanger 10 has a head part 50 to which the treatment line 52 is connected. Solvent-saturated flow can be discharged through the treatment line 52 in order to prevent the contents of the heat exchanger 10 and the tubular reactor 14 from being polluted or by-products concentrated.

In the embodiment shown in FIG. 2, the tubular reactor 14 is located, compared to the embodiment shown in FIG. 1, outside the heat exchanger 10. In this case, the flow past the discharge line 32 is fed through the supply line 54 to the heat exchanger 10, where the flow is cooled by the heat exchange elements 36 In this case, the flow can pass through the heat exchanger 10 in particular linearly and be fed through the return line 56 again to the tubular reactor 14 in order to perceive the resulting reaction body. Likewise, the solvent that is separated in separation device 58 (FIG. 3) from the product stream sampled through the exhaust line 32 can again be fed through the recycling line 60 to the tubular reactor 14. In the embodiment shown in FIG. 2, the tubular reactor 14 is located in line 60 recycling, and part of the line 60 recycling forms a section 16 of the pipe of the tubular reactor 14.

In the installation shown in FIG. 3, the heat exchanger 10 shown in FIG. 1, which has a tubular reactor 14, is connected to a separation device 58. Alternatively, the heat exchanger 10 can be replaced by the system shown in FIG. 2. The discharge line 32 of the tubular reactor 14 is connected through a separation line 64 to a separation device 58. In the separation device 58, the product fed through the separation line 64 is purified, for example, by distillation and separated into at least two partial streams. The cleaned product leaves the separation device 58 through the finished product line 66 in order to store the product and / or to further refine and / or pack. The separated components, which are saturated in particular with a solvent and have a catalyst and / or unreacted starting materials, are fed through a recycling line 60 and a heat exchanger 10 to a tubular reactor 14.

Claims (37)

1. Tubular reactor for multiphase polymerization, including at least - pipe section (16) for radially restricting the reactor volume between the inlet (18) and the outlet (20), - a mixer (22) to create a flow (27) in the axial direction of the pipe segment (16), moreover, the mixer (22) is of such dimensions and can be operated in such a way that centrifugal force can be imparted to the stream (27), which creates a concentration distribution in the radial direction inside the pipe section (16), and - an exhaust line (32) for diverting the radially inner part (30) of the stream (27, 28), moreover, the discharge line (32) is made with the possibility of movement in the axial direction with respect to the pipe segment (16). 2. A tubular reactor according to claim 1, characterized in that a biphasic layered rotating stream (28) can be created at least with a stirrer (22) in the separation region (46) coordinated with the outlet (20) within the pipe section (16) in two parts (30, 48) of various concentrations. 3. Tubular reactor according to claim 1 or 2, characterized in that the mixer (22) is located next to the inlet (18), and a first supply line (38) for introducing the first source product and a second feed line (40) for introducing the second the initial product and / or catalyst, the first feed line (38) and the second feed line (40) ending in the pipe segment (16). 4. The tubular reactor according to any one of paragraphs. 1-3, characterized in that the outlet line (32) is immersed inside the pipe section (16) in the concentrated radially inner part (30) of the stream (27, 28). 5. The tubular reactor according to any one of paragraphs. 1-4, characterized in that the mixer (22) is connected to the shaft (24), and the shaft (24) is configured to enter the tubular reactor (14) through the input (25) of the shaft, and the input (25) of the shaft is configured washing with a solvent. 6. The tubular reactor according to any one of paragraphs. 1-5, characterized in that for the ratio of the inner diameter D of the pipe segment (16) to the outer diameter d of the mixer (22), the following is true 1.0001≤D / d≤1,300. 7. The tubular reactor according to any one of paragraphs. 1-6, characterized in that the exhaust line (32) has a cooling device for cooling the exhaust line (32), and the cooling device has a double-walled shell pipe for conducting a cooling medium. 8. A heat exchanger with a tubular reactor (14) for multiphase polymerization, wherein the tubular reactor (14) includes at least - pipe section (16) for radially restricting the reactor volume between the inlet (18) and the outlet (20), - a mixer (22) to create a flow (27) in the axial direction of the pipe segment (16), moreover, the mixer (22) is of such dimensions and can be operated in such a way that centrifugal force can be imparted to the stream (27), which creates a concentration distribution in the radial direction inside the pipe section (16), and - an exhaust line (32) for diverting the radially inner part (30) of the stream (27, 28), moreover, the tubular reactor (14) is located concentrically inside the heat exchanger (10), and the heat exchanger (10) in the radial direction outside the tubular reactor (14) has at least one heat exchange element (36) for heat removal, moreover, a tubular mixer (22) reactor (14) can create a loop-like flow (34) inside the heat exchanger (10). 9. A heat exchanger according to claim 8, characterized in that a biphasic layered rotating stream (28) with at least two can be created in the separation region (46), coordinated with the outlet (20), inside the pipe section (16), with at least two parts (30, 48) of various concentrations. 10. A heat exchanger according to claim 8 or 9, characterized in that the mixer (22) is located next to the inlet (18) and a first supply line (38) is provided for introducing the first source product and a second supply line (40) for introducing the second source product and / or catalyst, the first supply line (38) and the second supply line (40) ending in the pipe segment (16). 11. The heat exchanger according to any one of paragraphs. 8-10, characterized in that the outlet line (32) is immersed inside the pipe section (16) in the radially concentrated inner part (30) of the stream (27, 28). 12. The heat exchanger according to any one of paragraphs. 8-11, characterized in that the mixer (22) is connected to the shaft (24), and the shaft (24) is configured to enter the tubular reactor (14) through the input (25) of the shaft, and the input (25) of the shaft is configured washing with a solvent. 13. The heat exchanger according to any one of paragraphs. 8-12, characterized in that for the ratio of the inner diameter D of the pipe section (16) to the outer diameter d of the mixer (22), the following 1.0001≤D / d≤1,300 is valid. 14. The heat exchanger according to any one of paragraphs. 8-13, characterized in that the exhaust line (32) has a cooling device for cooling the exhaust line (32), and the cooling device has a double-walled shell pipe for conducting a cooling medium. 15. The heat exchanger according to any one of paragraphs. 8-14, characterized in that the discharge line (32) is arranged to move in the axial direction with respect to the pipe section (16). 16. Installation for multiphase polymerization, including at least a heat exchanger (10) for cooling a fluid containing a solvent, - a separation device (58) for separating the product and - recycling line (60) connected to the output of the separation device (58) and to the heat exchanger (10), moreover, the heat exchanger (10) is made according to any one of paragraphs. 8-15 or contains a tubular reactor according to any one of paragraphs. 1-7 and / or the recycling line (60) has a tubular reactor (14) according to any one of paragraphs. 1-7, and the outlet line (32) of the tubular reactor (14) is connected to the input of the separation device (58). 17. The method of multiphase polymerization, which includes the steps: - mixing the first starting product with the second starting product and / or catalyst for polymerization to form the product in a solvent using a stirrer (22), - imparting centrifugal force to at least the aforementioned product and solvent using the same mixer (22) and - selection of concentrated radially inner part (30) of the stream (27, 28), moreover, said product has a lower density than the solvent. 18. The method according to p. 17, characterized in that when the centrifugal force is applied, a rotating stream (28) is created, and the rotating stream (28) is a two-phase layered rotating stream (28) with at least two parts (30, 48) various concentration. 19. The method according to p. 17 or 18, characterized in that at least the solvent is cooled, and at least the solvent after applying a centrifugal force and after selection of the concentrated radially inner part (30) of the stream (27, 28) is supplied in a loop-shaped stream (34) to at least one heat exchange element (36) for heat removal, and the loop-shaped stream (34) is created using the same mixer (22). 20. The method according to any one of paragraphs. 17-19, characterized in that the mixer (22) is operated in such a way that for the ratio c = w _tan ² / ((d / 2) ⋅g), where w _tan is the tangential velocity at the outer edge of the mixer (22), d is the outer diameter of the agitator (22) and g is the acceleration of gravity, valid c≥10. 21. The method according to any one of paragraphs. 17-20, characterized in that a tubular reactor (14) according to any one of paragraphs is used. 1-7 and / or heat exchanger (10) according to any one of paragraphs. 8-15 and / or installation (62) according to claim 16.

Images